Method of producing polymer compositions based on chlorinated polyethylene

ABSTRACT

In a method for producing a polymer composition by contacting A. a polymer component selected from the group consisting of chlorinated polyethylene and a mixture consisting of a major amount of chlorinated polyethylene and a minor amount of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinyl acetate copolymer rubber, with B. a monomer mixture comprising B1. AT LEAST ONE OF STYRENE, ALPHA-METHYL STYRENE, TERTIARY BUTYL STYRENE AND CHLOROSTYRENE, AND B2. AT LEAST ONE OF ACRYLONITRILE AND METHACRYLONITRILE UNDER POLYMERIZATION CONDITIONS TO FORM AN INTERPOLYMER OF THE COMPONENTS (A) and (B), the improvement which comprises suspending polymer component (A) and monomer component (B) in the form of fine particles in an aqueous medium.

United States Patent [191 Takahashi et al.

[ June 3, 1975 METHOD OF PRODUCING POLYMER COMPOSITIONS BASED ON CHLORINATED POLYETHYLENE [75] Inventors: Akira Takahashi; Hiroo Kojima;

Masao Ogawa, all of Tokyo; Hiroshi Osuka, Yokohama; Shoichi Kobayashi, Tokyo, all of Japan [73] Assignee: Showa Denko Kabushiki Kaisha,

Tokyo, Japan [22] Filed: Apr. 16, 1971 [21] Appl. No.: 134,826

Related US. Application Data [63] Continuation-impart of Ser. No. 784,517, Nov. 22, 1968, Pat. No. 3,673,279, which is a continuation-in-part of Ser. No. 339,899, Jan. 24, 1964, Pat. No. 3,496,251.

'52 us. c1 260/878 R [51] Int. Cl C08f 15/00; COSf 1/11 [58] Field of Search 260/878 R [56] References Cited UNITED STATES PATENTS 3,496,251 2/l970 Takahashi et al 260/878 R 3,558,745 l/l97l Ogawa ct al. 260/878 R Primary ExaminerJoseph L. Schofer Assistant ExaminerAlan Holler Attorney, Agent, or Firm-Sherman & Shalloway [57] ABSTRACT In a method for producing a polymer composition by contacting A. a polymer component selected from the group consisting of chlorinated polyethylene and a mixture consisting of a major amount of chlorinated polyethylene and a minor amount of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinyl acetate copolymer rubber, with B. a monomer mixture comprising b,. at least one of styrene, alpha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b at least one of acrylonitrile and methacrylonitrile under polymerization conditions to form an interpolymer of the components (A) and (B), the improvement which comprises suspending polymer component (A) and monomer component (B) in the form of fine particles in an aqueous medium.

6 Claims, No Drawings 1 METHOD OF PRODUCING POLYMER COMPOSITIONS BASED ON CHLORINATED POLYETHYLENE The polymer compositions obtained in accordance 'with the invention method comprehend the interpolymers based on chlorinated polyethylene and the blended compositions of such interpolymers with other polymers. These compositions all possess conjointly the desirable properties such as excellent impact strength,

weatherability, resistance to attack by chemicals, flame resistance, resistance to soiling as well as good processability and other properties which will be described hereinafter, thus making these compositions highly suitable for molding purposes.

A particular feature of the invention method resides in the fact that an interpolymer is formed by contacting under polymerization conditions the starting materials, i.e., the base polymer and the monomer components, which are in a state of suspension separately in the same aqueous medium and, in addition, in that this operation can be carried out commercially very smoothly and with great efficiency.

An object of the present invention is therefore to provide a new and commercially valuable method of producing polymer compositions. Another object is to provide polymer compositions which possess excellent properties as resins for molding purposes. Other objects and advantages will become apparent from the following description.

The method of producing the interpolymers according to the invention will be first described.

A number of methods of producing interpolymers have been known in the past. The production of an interpolymer is usually carried out by the technique known as graft polymerization, i.e., a method of polymerizing a monomer or monomers on a trunk polymer. The polymer which has been formed in this manner is usually referred to as a graft copolymer. However, strictly speaking, this is a homogeneous polymer composition comprising an intimate mixture of the copolymer consisting of a trunk polymer having a monomer grafted thereon, the base polymer used as the trunk polymer, and the homopolymers of monomer or monomers which have been used; i.e., this is an interpolymer. What is referred to herein as an interpolymer or graft copolymer is meant to be such a homogeneous polymer composition.

The techniques of graft polymerization which have been known heretofore include such methods as bulk, solution, emulsion and suspension polymerization methods as well as the two-stage polymerization method which consists of a suitable combination of two of the foregoing methods. The shortcomings of these conventional methods are outlined below.

In the bulk polymerization method, a requisite condition is that the trunk polymer used must be soluble in the monomer. Therefore, the degree to which the truck polymer is soluble in the monomer imposes a restriction on the proportion in which the two components are used and the polymerization operation. Again, when the viscosity of the solution is very high, the agitation thereof as well as the control of the polymerization temperature resulting from the influence of the reaction heat is not only difficult, but also since the resulting polymer frequently contains a considerable amount of residual monomers and its complete removal is difficult, causes degradation of the quality of the product.

While the shortcoming of the aforesaid bulk polymerization is not seen in the case of the solution polymerization method, it has instead disadvantages which are very great from the standpoint of commercial operations in that there is the need for a recovery operation of the solvent that is used and that a loss of the solvent is involved.

In the emulsion polymerization method a latex of the base polymer must be used. Further, the use of a considerably great amount of an emulsifier and a salting agent for separating the resulting polymer is required. Thus, not only is the operation complicated, but also there is the drawback that the emulsifier and salting agent used remains in the product as impurities.

Since in the suspension polymerization method the polymerization reaction is carried out in an inert medium such as water, the control of the temperature is simple and, in addition, the quality of the resulting product is uniform.' However, for forming the suspension system it is necessary to either dissolve the base polymer completely in the monomer or impregnate the former with the latter and effect its homogeneous swelling before the base polymer and monomer are suspended in the medium. Thus, the preliminary steps involved are troublesome. Moreover, it can only be practiced within the limits of the degree of solubility of th base polymer in the monomer. Accordingly a restriction is imposed on the weight ratio in which the two components can be used and therefore does not permit a free choice. Again, even though the ratio of the two components is within the degree of solubility of the polymer, similar difficulties are encountered as in the case with the aforesaid bulk polymerization method when the viscosity of the solution is high.

Thus, as hereinabove described, it was necessary in the conventional methods for producing an interpolymer for molding use that the base polymer and monomer were in state where the two components were either mutually dissolved or intimately mixed prior to their being submitted to the polymerization conditions. Further, only by doing this was it possible to obtain the intended interpolymer.

'In contradistinction, the method of producing an interpolymer according to the present invention fundamentally comprises contacting the base polymer and monomer under polymerization conditions in a state wherein the two components are separately suspended as fine particles in the same aqueous medium. That is, the base polymer and the monomer are not in either a homogeneously mixed or mutually dissovled state prior to the polymerization reaction. According to the invention method, the particles of the base polymer and the particles of the monomer, which are in suspension in the same aqueous medium, are brought into contact with each other by, stirring for example, and the latter penetrates into the former while being polymerized to thereby complete the formation of a homogeneous interpolymer. That a desirable interpolymer can be obtained by a method such as hereinabove described is truly surprising when compared with the conventional methods.

Various advantages which could not be obtained by the conventional methods are afforded by the present invention such as that equipment and operations for a preliminary dissolving step are unnecessary; that suspension is readily accomplished without encountering any difficulty such as is experienced in suspending a high viscosity solution; and that the ratio in which the two components are contained can be freely chosen without being limited by the degree of solubility of the base polymer in the monomer. Again, there is, of course, no need for using an organic solvent, and the control of the reaction temperature is readily accomplished.

Before describing the base polymer component and the monomer components that are used in the invention method, a preferred mode for forming the interpolymer will be described.

The base polymer component and the monomer components can be suspended in the aqueous medium either at the same time but separately from each other or one after the other. Alternatively, an. aqueous suspension of each of the components can be prepared in advance and thereafter the so prepared suspensions can be combined. For obtaining a good suspension, vigorous stirring is performed, and preferably a suspension stabilizer or suspending agent is used. The conventional suspension stabilizers, for example, water-soluble high molecular weight compounds such as polyvinyl alcohol, polyalkylene oxide and cellulose derivatives and powders of the difficultly soluble inorganic salts such as calcium carbonate, calcium phosphate are useable and magnesium phosphate. The amount in which the suspension stabilizer is used is suitably from 0.05 to 1% based on the weight of the water. While any particle size of the base polymer will do as long as it is of sufficient fineness for forming a suspension, it is preferably of 5-150 Tyler mesh size, and still more preferably of -48 Tyler mesh size in view of the stability of the suspension and the qualityof the product. The amount of water to be used is suitably 0.8-10 times the total weight of the base polymer component and monomer component used in the polymerization reaction. While the stability of the suspension is maintained as the amount of water increases, the use of about 0.8-3 times is preferred from the standpoint of commercial economy.

The polymerization reaction is carried out in customary manner by the action of heat or the action of a polymerization initiator. It is suitably carried out in the presence of a polymerization initiator and a chain transfer agent. The initiators which are useable are the known organic peroxide type catalysts and the azo compound type catalysts. Especially convenient are the former, examples of which include lauroyl peroxide, tertiary butyl peracetate, tertiary butyl benzoate and benzoyl peroxide. As the chain transfer agent, normaldodecyl mercaptan, tertiary dodecyl mercaptan and others can be used. From the standpoint of convenience of operation and satisfactory results that are obtained, the polymerization initiator is preferably mixed in advance in the monomer component prior to its suspension in the aqueous medium. In addition to the initiator and the chain transfer agent, additives such as chlorinated paraffin, hardened wax, liquid paraffin and higher fatty acids can be added, if desired, for improving the processability and impact strength of the product. A polymerization temperature in the range of 50150C. is convenient. Various other means that are used in the conventional suspension polymerization method may also be employed.

As a result of operating in the manner hereinbefore described, an interpolymer is obtained according to the invention method, wherein the total amount of the base polymer component and the monomer component used is nearly completely polymerized. The resulting interpolymer ordinarily retains practically the same particulate form as that of the base polymer used as the starting material. No particles of a homopolymer or copolymer consisting of only the monomer component used are formed. The resulting interpolymer can be readily separated from the aqueous medium by means of, filtration, for example. After water-washing, if desired, the particles are dried, thereby obtaining the intended interpolymer as a final product.

The distinctive properties of the base polymer component and the monomer component that are used in the present invention as well as that of the interpolymers obtained therefrom will now be described hereinbelow.

The base polymer component (A) is either chlorinated polyethylene or a mixture comprising a major amount of chlorinated polyethylene and a minor amount of a copolymer selected from an ethylenepropylene copolymer rubber (EPM), an ethylenepropylene-nonconjucated diene terpolymer rubber (EPDM) and an ethylene vinyl acetate copolymer rubber (EVA) (vinyl acetate content 5-60 weight On the other hand, the monomer component (B) used is a mixture of two kinds of monomers, one kind of monomer (1),) being selected from styrene, alpha-methylstyrene, t-butyl styrene and chlorostyrene, the other kind of monomer (b being selected from acrylonitrile and methacrylonitrile. The interpolymer which is formed by submitting these components (A) and (B) in a specified weight ratio to polymerization conditions in an aqueous suspension system possesses excellent impact strength when used as a thermoplastic molding resin. The weight ratio of the component (A) to component (B) to be employed ranges from 10:90 to :10, while the weight ratio of ingredient (b,) to ingredient (b is selected from the range 10:90 to 90:10. Generally speaking, the impact strength of the resultinginterpolymer becomes greater in proportion as the amount of component (A) becomes greater. On the other hand, the tensile strength of the interpolymer becomes greater in proportion as the amount of component (B) becomes greater. When the interpolymer is to be used as a molding resin, a weight ratio of (A):(B) ranging from 10:90 to 50:50 is most suitable.

As a typical example, first the case where the component (A) is chlorinated polyethylene and component (B) is a mixture of acrylonitrile and styrene will be described. The chlorinated polyethylene is prepared by the chlorination of polyethylene with chlorine. In the invention, a chlorinated polyethylene of a degree of chlorination (weight content of bonded chlorine) of l0-50%, and more preferably of 20-40%, is used. Further, since a chlorinated polyethylene obtained by the chlorination of polyethylene having a weight average molecular weight exceeding 100,000 provides an interpolymer having an especially high impact strength,

such a chlorinated polyethylene is particularly suitable. The preparation of a desirable interpolymer by the use of a base polymer having such a high molecular weight is only possible in the case where the hereinbefore described invention suspension system technique is used. This is extremely difficult in the case of the conventional solution, bulk and suspension techniques due to the high viscosity that is ascribable to the high molecular weight polymer.

When an interpolymer is to be made as hereinabove described using chlorinated polyethylene as the base polymer (A) and a mixture of acrylonitrile and styrene as the monomer component (B) a most valuable product is provided when the weight ratio of AB ranges from :90 to 90:10, and preferably 10:90 to 50:50, and the weight ratio of acrylonitrile: styrene ranges from 10:90 to 35:65.

The so obtained interpolymer, i.e. a thermoplastic resin, possesses a high impact strength, tensile strength and flexural strength and has good processability and dimensional stability. Furthermore, it excels in weatherability, flame resistance and resistance to soiling.

l-leretofore, as thermoplastic three-component polymeric compositions, there are known, for example, those generally referred to as the ABS polymers, which are either copolymers of polymeric or copolymeric mixtures consisting of acrylonitrile, styrene and butadiene. While these ABS polymers and the other threecomponent polymeric compositions of the same class are all comparatively good in their impact strength and dimensional stability, their flame resistance, resistance to burning, weatherability and processability are however not yet quite satisfactory. In contrast, the aforesaid three-component polymeric composition of the present invention does not possess these shortcomings of the ABS polymers. The reason therefor is believed to be due to the fact that in polybutadiene, the base polymer of the ABS resin, a double bond is present which causes the degradation of this resin, whereas such a double bond is not essentially present in the resin of present invention.

As the ingredient (in) of the monomer component (B), alpha-methyl styrene, t-butyl styrene or chlorostyrene can be substituted for all or part of the styrene. By such a substitution a still greater improvement can be had in the thermal stability of the product. Further, methacrylonitrile can be substituted for all or part of the acrylonitrile as the other ingredient (b ln preparing an interpolymer by the invention method, a mixture comprising a major amount of chlorinated polyethylene and a minor amount of a copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinyl acetate copolymer rubber can be used instead of the aforesaid chlorinated polyethylene. The ethylene-propylene copolymer rubber and the ethylene-propylene-nonconjugated diene terpolymer rubber have been generally well known hitherto as EPM and EPDM, respectively. These are both a rubbery polymer having 35-80% by weight of ethylene units and a specific gravity of about 0.83-0.85.

It has been found that by using as the base polymer component EPM, EPDM or EVA in conjuction with the chlorinated polyethylene, an interpolymer having improved low temperature fragility can be obtained when compared with the case where chlorinated polyethylene is used alone. When EPM, EPDM or EVA is merely blended in an interpolymer obtained by the use of chlorinated polyethylene alone, there is an improvement in the low temperature fragility but there is the disadvantage that a marked decline takes place in the impact strength at room temperature. The proportion in which the EPM, EPDM or EVA is contained in the base polymer component is most desirably from 10 to 50% by weight.

Thus, as fully described hereinbefore, various desirable thermoplastic polymer compositions can be obtained according to the present invention by a suitable combination of the classes and weight ratios of the base polymer component and the monomer component.

Further, in accordance with the invention, a modified mode of preparing these desirable thermoplastic resin is provided which comprises preparing an interpolymer wherein the amount used of base polymer component is great and the amount of monomer component is small, blending with the so obtained interpolymer a homopolymer or copolymer separately prepared from only the monomer component, thereby diluting the proportion contained of the base polymer component to the degree desired. Since the foregoing interpolymer is already incorporated with component (B), its compatibility with the polymer consisting solely of component (B) is high, with the consequence that a homogeneous blend can be readily obtained. The blending can be accomplished in customary manner, using, for example, an extruder, mixer or mixing rolls. For brevity this method is referred to as either the graft-blend procedure or master batch procedure. The properties of the blended composition obtained by this method are about the same as those of an interpolymer whose weight ratio of component (A) to component (B) is identical. The rigidity is rather higher. For carrying out the graft-blend procedure in a desirable manner, an interpolymer master batch is prepared with the weight ratio of component (A) to component (B) ranging from 10:90 to :10, following which a separately prepared polymer consisting of only component (B) is blended therewith to form a composition in which the overall weight ratio (A):(B) is in the range of 5:95 to 50:50.

Since in the master batch procedure a master batch of the inter-polymer containing the base polymer component in a high concentration is used and a separately prepared polymer consisting of only the monomer component is blended with the foregoing master batch in varying amounts, as required, thermoplastic resins of various desired grades can be provided. Thus it is convenient and advantageous from the standpoint of commercial production. A method such as described is only possible by the method of producing an interpolymer in a suspension system in accordance with the present invention. In the conventional solution, bulk and suspension polymerization methods, when the concentration of the base polymer component was high, it was impossible to carry out the production for the reason of the limited solubility of the base polymer component in the monomer component. Even when the former was soluble in the latter, the viscosity would become exceedingly high to render the operation difficult to carry out.

if desired, the conventional additives such as a plasticizer, stabilizer, lubricant and others may be added to the interpolymer composition or blended polymer composition obtained by the invention method. For example, if a small amount of a flame retardant such as antimony trioxide, hexabromobenzene, perchloropentacyclodecane and decachlorobiphenyl is incorporated in the invention polymer composition, its good fire resistance can be further enhanced. Since the fire resistance of the conventional ABS resins is generally low, the addition of a flame retardant such as hereinabove described has been attempted to make up for this deficiency. However, since the flame retardant must be added in a considerably large amount to obtain a desirable fire resistance, the various desirable properties which are intrinsically possessed by the ABS resins are greatly impaired. This does not happen in the case of the invention polymer.

In one application of the thermoplastic polymer composition obtained by the invention method, a polymer or copolymer of vinyl chloride is blended therewith. This likewise provides a molding resin which has a desirable impact strength and fire resistance. The polymer or copolymer of vinyl chloride used in this case is the usually available ordinary polyvinyl chloride resin, which is incorporated in the composition in an amount of l-70% by weight, and preferably -30% by weight. Practically no decline in the properties of the composition was noted as a result of the incorporation of the polyvinyl chloride resin.

The following examples are given for further illustration of the invention. Unless otherwise specified, the parts and percentages in the examples are on a weight basis. The properties of the resulting products were measured in accordance with the following methods:

ASTM

Properties Unit D256-56T D638-58T do. DlZ38-57T (190C, 10 kg) Dl525-58T D648-56 ft-lb/inch Impact strength kg/cm Tensile strength Elongation Flow rate g/lO min Vicat softening point Heat distortion temperature EXAMPLE I Recipe (1) P L ar s Chlorinated polyethylene powder 24 (weight average molecular weight of the starting polyethylene 150,000,

degree of chlorination 30 Polyvinyl alcohol (degree of saponification 95 0.4

Water (ion-exchanged water) Tertiary dectyl mercaptan (chain trans er agent) After the resulting polymer was cooled, it was separated from the water, water-washed and dried. Transparent particles of only the styrene-acrylonitrile copolymer could not be seen among the so obtained poly mer particles. The particle size distribution of the chlorinated polyethylene before its polymerization and that of the resulting polymer are shown in the following table.

Table 1 Resulting Particle size Starting chlorinated polymer (mesh) Polyethylene 10 on 3 3 l0 2O 82 77 20 32 l4 17 32 pass 1 3 As is apparent from Table 1, it is believed that the monomeric styrene and acrylonitrile have been polymerized by having been either absorbed or impregnated into the interstices of the chlorinated polyethylene powder, since no appreciable change is noted in the particle size distribution between the starting chlorinated polyethylene and the resulting polymer. Two parts of dibasic lead phosphite were added to the resulting polymer as a stabilizer and then test pieces were made therefrom by pelletizing at 200C. with a 20-mm extruder. When the impact strength was then measured, it was 1 1.3 ft-lb/inch Izod-notch (room temperature). Further, the flow rate was 3.0 g/lO min. when measured with a melt indexer. On the other hand, the tensile strength was 345 kg/cm CONTROL I In this experiment the base polymer was dissolved in the monomer, following which the so obtained solution was suspension polymerized.

Components of following recipe were charged to a dissolving tank and dissolved with stirring.

Parts Chlorinated polyethylene 12 (weight average molecular weight of the starting polyethylene 150,000. degree of chlorination 30 Styrene monomer 53 Acrylonitrile monomer 21 Liquid paraffin 4 Tertiary butyl peracetate 0.03

Tertiary dodecyl mercaptan 0.05

Next, the so obtained solutionwas added to the following suspension system and suspended therein.

Parts Water (ion-exchanged water) I Polyvinyl alcohol 4 After purging the system with nitrogen, the temperature was raised to 105C. but during this time aggregation of the suspension took place to convert it into a lumpy mass thereby rendering it impossible to continue the polymerization operation.

CONTROL II This experiment illustrates the case where the base polymer and a polymer of the monomer were blended.

A chlorinated polyethylene as used in Example I, liquid paraffin and an acrylonitrile-styrene copolymer obtained by polymerizing at the same ratio as in Example I were mixed such that the composition would be identical to that of Example I, after which the mixture was pelletized by extruding from a -mm extruder at 200C. When the properties of this blend were measured as in Example I, the impact strength was 0.9 ftlb/inch, the flow rate was 2.5 g/l0 min. and the tensile strength was 270 kg/cm Further, when this same composition was blended for 10 minutes at 170C. with 3- inch rolls, only results which were about the same were obtained.

Thus, the polymer obtained in Example I, above, in accordance with the invention method possesses superior properties as compared with those of a mere mixture of the polymers, and it is believed that the polymer obtained according to the invention method is a partly graft-copolymerized homogeneous polymer composition.

EXAMPLE II A polymer was obtained by operating as in Example I, using the Recipes (I) and (2), below.

The relationship between the particle size of the chlorinated polyethylene prior to its polymerization and that of the product is shown in Table 2, below.

Table 2 Starting chlorinated Resulting Particle size polyethylene polymer (m s 10 on 2 4 IO 20 71 66 2O 3'2 24 26 32 pass 3 4 The resulting'product was water-washed and dried. Then, after adding 2 parts of dibasic lead phosphite, properties of the product were measured as in Example I. With respect to impact strength, the product did not break by the Izod-notch method at room temperature. The flow rate was 0.3 g/IO min., and the tensile strength was 190 kg/cm EXAMPLE III The experiment was operated as in Example I, using the following Recipes (I) and (2):

After purging the autoclave with nitrogen, the reaction was carried out for 4 hours at C. and for 2 hours at C., followed by water-washing and drying the reaction product to obtain a polymer.

The relationship between the particle size of the chlorinated polyethylene prior to its polymerization and that of the resulting product is shown in the following table.

Table 3 Starting chlorinated Resulting Particle size polyethylene polymer (mesh) 20 on 9 l l Table 3-Continued EXAMPLE IV The experiment was carried. out as in Example I,

St rt i zgi Resulting using the following Recipes (1) and (2). Particle size polyethylene polymer 20 32 22 23 32 48 67 64 Recipe (1) 48 pass 2 2 Parts Chlorinated polyethylene powder 50 (weight average molecular weight of Separately, an acrylonltrlle-styrene copolymer was starting polyethylene 150,000, prepared with the following Recipe (3). degree of chlonmmo 25 Water (ion-exchanged water) 200 Polyvinyl alcohol 0.6 Recipe (3) Parts Acrylonitrile monomer 25 Styrene monomer 75 Water (ion-exchanged water) 100 Recipe (2) Lauroyl peroxide 0.4 Parts Tertiary butyl benzoate 0.05 Tertiary dodecyl mercaptan 0.3 Styrene monomer 40 Tertiary calcium phosphate l.0 Acrylonitrile monomer 5 Anionic surfactant 0.005 Methacrylonitrile monomer 5 Mineral oil 7 Lauroyl peroxide 0.2 Tertiar but I benzoate 0.02 The components of the foregomg Recipe (3) were Tertiar; dod ecyl mercaptan 0.05 charged to a 5liter reactor and, after purging the reactor with nitrogen, the reaction was carried out for 4 hours at 80C. and for 2 hours at 140C. After comple- After purging the autoclave with nitrogen, the reaction of the polymerization reaction, the product was 0 tion was carried out for 4 hours at 80C. and for one washed with water and dried. 3 hour at 140C. The resulting product was washed with The polymeric product obtained by means of Recipes water and dried to obtain a polymer. (1) and (2) and the acrylonitrile-styrene copolymer 0b- The relationship between the particle size of the tained by means of Recipe (3) were blended with a chlorinated polyethylene prior to its polymerizatlon ZO-mm extruder. The properties of the resulting polyand that of the resulting product is shown in Table 6, mer composition are shown in Table 4. below.

Table 4 Concentration of the chlorinated lmpact Tensile Vicat Elongation Elongation polyethylene after strength strength Flow rate softening E, E2*

blending (ft-lb/ point (70) inch notch) (kg/cm (g/lO min.) (C) 7:) (7Q 15 1.5 402 7.2 105 l3 l3 20 1.8 355 6.0 104 41 25 5.4 305 4.6 l02 73 44 30 11.7 250 3.5 99 I03 I00 ABS resin** 79 361 H) 103 31 6 Elongation after exposure for 200 hours in :1 Wcuthcr-O-Mctcr. Commercial product (comparison) The experiment was carried out as hereinabove de- Table 6 scribed, using, however, as the chlorinated polyethylene one whose starting polyethylene was of a weight av- Starting chlorinated Resulting erage molecular weight of 90,000. A polymer composi- 5 zg s i P 023 1 P a l u l0 tron having the following properties was obtained.

20 on 5 6 20 32 20 2l 32 48 73 71 Table 5 48 pass 2 2 v I 1 con t f This product and an acrylonitrile-styrene copo ymer the chlorinated Impact prepared in accordance with the Reclpe (3) g1ven m Y P 'l Example III were blended in amounts such as to result after blending (ft-lb/inch strength Flow rate notch) (kglcm (g/lO min.) In a chlorinated polyethylene concentrat1on after blending of 23%, using a 20-mm extruder. The proper- $8 8'2 328 ties of the so obtained composition are shown as fol- 25 1.0 285 11 lows: 30 2.0 225 8 Impact strength 7 5.0 ft-lb/inch notch Continued Tensile strength 330 kg/crn Flow rate 5.5 g/l() min.

EXAMPLE V In contrast to the procedure of Examples I-IV in this experiment a suspension of the starting monomer components were prepared first. Thus, the following monomer components were first charged to a 50-1iter autoclave and a suspension system was prepared by mixing the components with stirring.

Parts Styrene monomer 28 Acrylonitrile monomer 7 Mineral oil 1 l Lauroyl peroxide 0.15 Tertiary butyl perbenzoate 0.015 Tertiary dodecyl mercaptan 0.035 Water (ion-exchanged water) 300 Polyvinyl alcohol 0.8

This was followed by adding 65 parts of a chlorinated polyethylene powder (weight average molecular weight of the starting polyethylene 300,000, degree of chlorination 32%) to the suspension system. The autoclave was then purged with nitrogen, and the reaction was carried out for 4 hours at 80C. and then for 1 hour at 140C. After completion of the reaction, the product was water-washed and dried to obtain a polymer.

The relationship between the particle size of the chlorinated polyethylene before its polymerization and that of the resulting product is shown in Table 7, below.

Table 7 Starting chlorinated Resulting Particle size polyethylene polymer (mesh) on 9 l l 20 32 22 21 32 48 67 65 48 pass 2 3 This product and an acrylonitrile-styrene copolymer prepared in accordance with the Recipe (3) given in Example III were blended in such amounts as to result in a concentration of the chlorinated polyethylene of 28% after blending, using a 65-mm extruder. The properties of the so obtained composition are as follows:

Impact strength (ft.-lb./inch notch) 5.7 Tensile strength (kglcm 265 Flow rate (g/lO min.) 4.2

EXAMPLE VI The experiment was operated as in Example I, using the following Recipes (1) and (2).

Recipe (1) Path Chlorinated polyethylene powder 50 (weight average molecular weight of starting polyethylene 300,000.

After purging the autoclave with nitrogen, the reaction was carried out for 3 hours at C. and for 2 hours at C., the product being then water-washed and dried.

Separately, an acrylonitrile-styrene-alpha-methyl styrene ternary copolymer was prgpared in accordance with the following Recipe (3).

Recipe (3) Parts Acrylonitrile monomer 25 Styrene monomer 68 Alpha-methyl styrene monomer 7 Water (ion-exchanged water) Lauroyl peroxide 0,5 Tertiary butyl benzoate 0.05 Tertiary dodecyl mercaptan 0.2 Calcium tertiary phosphate" 1.4 Anionic surfactant 0.007

The components were charged to a reactor and, after purging the reactor with nitrogen, the reaction was carried out for 4 hours at 80C. and for 2 hours at 140C. After completion of the polymerization reaction, the product was washed with dilute hydrochloric acid, then water-washed and dried.

The polymeric product obtained previously in accordance with Recipes (1) and (2) and the acrylonitrilestyrene-alpha-methyl styrene ternary copolymer obtained as hereinabove described in accordance with Recipe (3) were blended in such amounts as to result in a chlorinated polyethylene concentration of 10%, using a 20-mm extruder.

The properties of the so obtained composition are as follows:

Impact strength (ft.-lb./inch notch) 1.0 Tensile strength (kglcm 430 Flow rate (g/lO min.) 0.8 Vicat softening point (C.) 1 l5 EXAMPLE VII The experiment was operated as in Example I, using the following Recipes (1) and (2).

Recipe 1 EXAMPLE V111 The experiment was operated as in Example I, using the following Recipes (1) and (2).

Parts Chlorinated polyethylene powder 40 (weight average molecular weight of starting polyethylene 300,000, Reupe (I) P r degree of chlorination 32 b I Chlorinated polyethylene powder 40 Fail-2&3;elzlopylEnL-IIOHCOHJUgdICd diene l0 (weight average moeculm weight of I starting pol eth lene 300,000, (tmdenime ROYALENE 30]) degree of c lon' r iation 40 waer ("mexchangel water) 200 Water (ion-exchanged water) 200 Polyvinyl alcohol 1 5 Polyvinyl alcohol 0,6

Recipe (2) Recipe (2) Parts Parts y n monomer 35 Styrene monomer 36 Acrylonitrile monomer 12.5 Chlorostyrene monomer l2 Tert ary butyl styrene 2.5 Acrylonitrile monomer 2 Tert ary butyl benzoate 0.15 Tertiary butyl benzoate 0.18 Tertiary dodecyl mercaptan 0.05 Tertiary dodecyl mercaptan 0.12

After purging the autoclave with nitrogen, the reac- After purging the autoclave with nitrogen, the reaction was carried out for 3 hours at 120C. and for 2 tion was carried out for 3 hours at 120C. and for 1 hours at 140C. The resulting product was then waterhour at 140C. The resulting product was then waterwashed and dried. washed and dried.

Separately, an acrylonitrile-styrene-tert.-butyl stye relationship between the particle size of chlorirene ternary copolymer was prepared in accordance nated polyethylene before its polymerization and that with the following Recipe (3). of the product are shown in Table 8.

Table 8 Recipe (3) Starting chlorinated Resulting Pans Particle size polyethylene product (mesh) Acrylonitrile monomer 25 Styrene monomer 70 0 20 on 10 12 Tertiary butyl styrene monomer 5 20 32 25 25 Water (ion-exchanged water) 100 32 48 64 6| Lauroyl peroxide 0.4 48 P1155 1 2 Tertiary butyl perhenzoate 0.05 Tertiary dodecyl mercaptan 0.4

figi i a 8 Separately, an acrylonltrlle-styrene-chlorostyrene ternary copolymer was prepared in accordance with the following Recipe (3).

The components were charged to a 5-liter reactor and, after purging the reactor with nitrogen, the reaction was carried out for 4 hours at 80C. and then for 50 Recipe (3) 2 hours at 140C. The resulting product was washed in Parts dilute hydrochloric acid followed by water-washing and Acrylomtnle monomer 20 y Styrene monomer 60 The product previously obtained in accordance with s ty onom e 8 -t I Recipes (1) and (2) and the acrylonl trile-styrene-tert. f g l gg gi water) 0.4 butyl styrene ternary copolymer obtamed heremabove Tertiary butyl perbenzoate 0.82 Tertiary dodecyl mercaptan 0. 1n accordance with Recipe (3) were blended in Calcium tertiary phosphate H) amounts such as to result in a total concentration of Anionic surfactant 0.005 chlorinated polyethylene and EPT of 27%, using a 20-min extruder.

The properties of the so obtained composition are as The Components were charge? a reactor follows. and, after purging the reactor with nitrogen, the reaction was carried out for 4 hours at C. and for 2 hours at C. After washing the resulting product in a d1- lmpa t r ngth (ft-l Ji n t 65 lute acid, it was water-washed and dried.

Flow rate (g/10 min.)

Tensile strength (kg/m2) 320 The product previously obtamed in accordance 1th v softening point c, 104 Recipes (1) and (2) and the acrylomtrile-styrene- Chlorostyrene copolymer obtained in accordance with Recipe (3) were blended in amounts such as to result in a chlorinated polyethylene concentration of 27% after blending, using a 20-mm extruder.

The so obtained composition had the following prop- EXAMPLE X The experiment was carried out as in Example I, ex-

cept that the following Recipes (1) and (2) were used. Recipe (l) erties. 5 Parts Ethylene-vinyl acetate copolymer powder 50 (a copolymer containing l7 of vinyl acetate was comminuted) notch) 3' Water (ion-exchanged water) 200 Flow rate (g/lO min.) 2.0 10 Vicat softening point (C.) 103 Polyvmyl alcohol Recipe (2) EXAMPLE IX Pam The experiment was carried out as in Example I, Styrene f p 40 Acrylomtrlle monomer l0 usmg the following Recipes (1) and 2). Mineral Oil 7 Tertiary butyl perbenzoate 0.15 Tertiary dodecyl mercaptan 0.05

Recipe (1 Af p ter purgmg the autoclave with mtrogen, the reaction was carried out for 3 hours at 120C. and 2 hours l 50 at 140C. The resulting product was then water-washed diene terpolymer powder (tradename ROYALENE 301 and dried. g1"? f The so obtained product was blended with the cog f ff fjg'gg 05p e 06 polymer obtained with Recipes l) and (2) in Example III and the acrylonitrile-styrene copolymer obtained with Recipe 3 in Example III in amounts such as to result in a concentration of the chlorinated polyethylene of 17% and a concentration of the ethylene-vinyl ace- Rwpe (2) Pans tate copolymer of 10%, the blending accomplished with a 20-mm extruder. i y e rtnolnomer 8 The properties of the so obtained composition are Cl'y On! ['1 e monomer Tertiary butyl perbenzoate 8.15 Shown as follows- Temary dodecyl mercaptan Impact strength (ft.-lb./inch notch) 6.8 Flow rate (g/lO min,) 4.0 Tensile strength (kg/cm 255 After purging the autoclave with nitrogen, the reaction was carried out for 3 hours at 120C. and for a further 2 hours at 140C. The resulting product was then EXAMPLE XI water-washed and dried. 40 A polymer prepared in accordance with the Recipes The so obtained product was then blended with the (1) and (2) of Example Ill and an acrylonitrile-styrene polymer obtained in Example III in accordance with copolymer prepared in accordance with Recipe (3) of Recipes (1) and (2) and the acrylonitrile-styrene co- Example III were blended with polyvinyl chloride and polymer obtained in Example III in accordance with aflame retardant assistant in the proportions indicated Recipe (3), using a 20-mm extruder, in amounts such in Table 10, using a 20-mm extruder. as to result after blending in a composition whose pro- The properties of the resulting compositions are portion of base polymers are as indicated in Table 9. shown below.

Table 9 Proportion of Base polymers after blending Impact strength Tensile (70) (fL-lbJin. notch) Flow rate strength CPE EPT +20c -10c I 3oc (g/lO min.) (kg/cm Table 10 (PE con- Heat centration PVC Impact Flow distortion after concen- Antimony strength rate tempera- Burnblending tration oxide (ft.-lb./ (g/ l (J ture g ("/1) (71) (71 in. notch) min.) (C) Test* 15 20 5 1.4 I2.() 83 equal to SE-l 22.5 40 0 3.8 7.8 H do. 22.5 0 6.8 7.4 69 do. 25 20 5.5 3.3 7.0 79 do.-

US. Underwriters Laboratory standard.

EXAMPLE x11 A polymer prepared in accordance with the Recipes (1) and (2) of Example III, an acrylonitrile-styrene copolymer prepared in accordance with Recipe (3) of Example III and, as flame retardants, hexabromobenzene and antimony trioxide were blended in amounts such as to result in concentrations of the chlorinated polyethylene of 26%, of the hexabromobenzene of 12% and of the antimony trioxide of 2.5% using mixing rolls.

The properties of the so obtained composition are as follows:

Impact strength (ftr-lbilin. notch) 4.3 Tensile strength (kg/cm") 290 Flow rate (g/lO min.) 7 2 Vicat softening point (C.) 102 We claim: 1. In a method for producing a thermoplastic resin composition by contacting A. a polymer component selected from the group consisting of chlorinated polyethylene of a degree of chlorination of 10-50% and a mixture consisting of 5090% by weight of said chlorinated polyethylene and 10-50% by weight of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinylacetate copolymer rubber, with B. a monomer mixture comprising b at least one monomer selected from styrene, al-

pha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b at least one monomer selected from acrylonitrile and methacrylonitrile under polymerization conditions in the presence of a polymerization initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separation from each other in an aqueous medium, said component (A) having a particle size of -l50 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about :90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.

2. In a method for producing a thermoplastic resin composition by contacting A. a polymer component comprising a chlorinated polyethylene of a degree of chlorination of l0-50%, with B. a monomer mixture comprising b at least one monomer selected from styrene, al-

' 20 pha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b at least one monomer selected from acrylonitrile and methacrylonitrileunder polymerization conditions in the presence of a polymerization initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separating from each other in an aqueous medium, said component (A) having a particle size of 5-150 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about 10:90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.

3. In a method for producing a thermoplastic resin composition by contacting A. a mixture consisting of 50-90% by weight of a chlorinated polyethylene of a degree of chlorination of 1050% and 10-50% by weight of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylenevinylacetate copolymer rubber, with B. a monomer mixture comprising b at least one monomer selected from styrene, al-

pha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b at least one monomer selected from acrylonitrile and methacrylonitrile under polymerization conditions in the presence of a polymerization initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separation from each other in an aqueous medium, said component (A) having a particle size of 5-150 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about 10:90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.

4. The method of claim 1 wherein said aqueous medium is used in an amount of 0.8-l0-fold the total weight of said components (A) and (B).

5. The method of claim 1 wherein the polymerization temperature ranges from 50 to C.

6. The method of claim 1 wherein said chlorinated polyethylene of component (A) is a polyethylene of a weight average molecular weight exceeding 100,000, which has been chlorinated to a degree of chlorination of l0-50%. 

1. IN A METHOD FOR PRODUCING A THERMOPLASTIC RESIN COMPOSITION BY CONTACTING A. A POLYMER COMPONENT SELECTED FROM THE GROUP CONSISTING OF CHLORINATED POLYETHYLENE OF A DEGREE OF CHLORINATION OF 10-50% AND A MIXTURE CONSISTING OF 50-90% BY WEIGHT OF SAID CHLORINATED POLYETHYLENE AND 10-50% BY WEIGHT OF COPOLYMER SELECTED FROM AN ETHYLENE-PROPYLENE COPOLYMER RUBBER, AN ETHYLENE-PROPYLENE-NONCONJUGATED DIENE TERPOLYMER RUBBER AND AN ETHYLENNE-VINYLACETATE COPOLYMER RUBBER, WITH B. A MONOMER MIXTURE COMPRISING B1. AT LEAST ONE MONOMER SELECTED FROM STYRENE, ALPHAMETHYL STYRENE, TEERTIARY BUTYL STYRENE AND CHLOROSTYRENE, AND B2. AT LEAST ONE MONOMER SELECTED FROM ACRYLONITRILE AND METHACRYLONITRILE UNDER POLYMERIZATION CONDITIONS IN THE PRESENCE OF A POLYMERIZATION INITATOR TO FORM AN INTERPOLYMER OF COMPONENTS (A) AND (B), THE IMPROVEMENT WHICH COMPRISES SUSPENDING SAID POLYMER COMPONENT (A) AND MONOMER COMPONENT (B) IN THE FORM OF FINE PARTICLES IN A STATE OF SEPARATION FROM EACH OTHER IN AN AQUEOUS MEDIUM, SAID COMPONENT (A) HAVING A PARTICLE SIZE OF 5-150 TYLER MESH, THE WEIGHT RATIO OF SAID COMPONENT (A) TO COMPONENT (B) RANGING FROM ABOUT 10:90 TO ABOUT 65:35, SAID POLYMERIZATION INITATOR BEING MIXED IN SAID COMPONENT (B) PRIOR TO ITS SUSPENSION IN THE AQUEOUS MEDIUM.
 1. In a method for producing a thermoplastic resin composition by contacting A. a polymer component selected from the group consisting of chlorinated polyethylene of a degree of chlorination of 10-50% and a mixture consisting of 50-90% by weight of said chlorinated polyethylene and 10-50% by weight of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinylacetate copolymer rubber, with B. a monomer mixture comprising b1. at least one monomer selected from styrene, alpha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b2. at least one monomer selected from acrylonitrile and methacrylonitrile under polymerization conditions in the presence of a polymerizatioN initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separation from each other in an aqueous medium, said component (A) having a particle size of 5-150 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about 10:90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.
 2. In a method for producing a thermoplastic resin composition by contacting A. a polymer component comprising a chlorinated polyethylene of a degree of chlorination of 10-50%, with B. a monomer mixture comprising b1. at least one monomer selected from styrene, alpha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b2. at least one monomer selected from acrylonitrile and methacrylonitrile under polymerization conditions in the presence of a polymerization initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separating from each other in an aqueous medium, said component (A) having a particle size of 5-150 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about 10:90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.
 3. In a method for producing a thermoplastic resin composition by contacting A. a mixture consisting of 50-90% by weight of a chlorinated polyethylene of a degree of chlorination of 10-50% and 10-50% by weight of copolymer selected from an ethylene-propylene copolymer rubber, an ethylene-propylene-nonconjugated diene terpolymer rubber and an ethylene-vinylacetate copolymer rubber, with B. a monomer mixture comprising b1. at least one monomer selected from styrene, alpha-methyl styrene, tertiary butyl styrene and chlorostyrene, and b2. at least one monomer selected from acrylonitrile and methacrylonitrile under polymerization conditions in the presence of a polymerization initiator to form an interpolymer of components (A) and (B), the improvement which comprises suspending said polymer component (A) and monomer component (B) in the form of fine particles in a state of separation from each other in an aqueous medium, said component (A) having a particle size of 5-150 Tyler mesh, the weight ratio of said component (A) to component (B) ranging from about 10:90 to about 65:35, said polymerization initiator being mixed in said component (B) prior to its suspension in the aqueous medium.
 4. The method of claim 1 wherein said aqueous medium is used in an amount of 0.8-10-fold the total weight of said components (A) and (B).
 5. The method of claim 1 wherein the polymerization temperature ranges from 50* to 150*C. 